CO2 Separation Using A Solid K-Fe Sorbent

ABSTRACT

A sorbent for CO 2  wherein K 2 CO 3  is supported on FeOOH.

This application claims priority to U.S. Patent Application Ser. No. 61/492,066, filed Jun. 1, 2011, and incorporates the same herein in its entirety by this reference.

BACKGROUND OF THE INVENTION

The invention relates generally to sorbents and, more specifically, to an inexpensive K—Fe-based sorbent developed using K₂CO₃ and nanoporous FeOOH.

People are increasingly concerned about the climate changes we have experienced; including the increases in global average air and ocean temperatures, rising sea levels, and widespread melting of ice caps and glaciers. Rising global temperatures could lead to many disasters including severe weather events, drought and flooding, and thus food supply shortfalls, lack of water security, deterioration of ecosystems, and spread of vector-borne diseases.

The main greenhouse gases associated with climate changes are carbon dioxide, methane, nitrous oxide and some halogenated compounds. The quantity of CO₂ emitted to the atmosphere due to human activities is much greater than those of other greenhouse gases. As a result, CO₂ makes the greatest contribution to the greenhouse effect despite its low unit globe warming potential. According to the latest analyses of the data from the global greenhouse gas monitoring network of World Meteorological Organization (WMO), the global concentration of CO₂ in the atmosphere reached a new high level in 2009, 386.8 ppm, which is ˜38% higher than those in pre-industrial times.

Net CO₂ emission reductions could be achieved by reducing energy consumption through increasing energy conversion efficiency, switching to less carbon-intensive fuels, and using alternative fuels. However, fossil fuels, such as coal, oil and natural gas, are likely to continue to be used for meeting more than 80% of total world energy demand in the coming decades due to their high energy densities and wide availabilities. The capture and storage of carbon dioxide will be the major method to be used for limiting CO₂ emissions from the combustion of fossil fuels in this century.

A variety of methods, such as membrane separation, absorption with a solvent, and cryogenics techniques, have been used to separate CO₂ from flue gases and other waste gas streams. These methods, however, are energy-intensive. Regenerable solid sorbents containing inexpensive alkali metals and alkali earth metals have attracted many people's attention since they could be regenerated with the heat recovered from the waste gas streams including flue gas and thus could provide cost-effective approaches to removal of CO₂ from flue gas in power plants. A major challenge in developing solid CO₂ sorbents is to find new multifunctional supporting materials for alkali chemicals such as potassium carbonate. Several studies have been conducted on separation of CO₂ from the simulated flue gas steams with K₂CO₃ supported by TiO₂, SiO₂, CaO, MgO and different porous matrices such as activated carbon, silica gel, aluminum oxide, and vermiculite under cyclic fixed-bed operation conditions along with the presence of H₂O. However, nanoporous FeOOH has not been tested by others as a supporting material for synthesis of a solid CO₂ sorbent. In this research, a new K—Fe solid sorbent has been developed using low-price potassium carbonate and nanoporous multifunctional FeOOH. The performance of the K—Fe sorbent on CO₂ sorption and desorption was evaluated using a fixed bed reactor under different operation conditions, and the associated sorption and desorption mechanism, thermodynamics as well as kinetics were investigated.

SUMMARY OF THE INVENTION

An inexpensive K—Fe-based sorbent was developed using potassium carbonate (K₂CO₃) and nanoporous FeOOH. Its CO₂ separation performance was investigated in a fixed bed tube reactor under different conditions. The K—Fe sorbent can increase CO₂ capture capacity by more than seventy times compared to pure solid potassium carbonate powder. The sorption capability of K—Fe sorbent reaches its peak when the content of K₂CO₃ in sorbent is 33.33% under the tested sorption conditions. The CO₂ sorption capacity of the sorbent increases with the increase of moisture in gas but it decreases dramatically with the elevation of sorption temperature. The total CO₂ capture capability of the K—Fe sorbent is ˜49 mg CO₂/g-sorbent at 60° C. within 10 vol-% moisture environment. The sorbent is regenerable and its multicycle sorption capability stays at approximately 30 mg CO₂/g sorbent when regeneration temperature is 125° C. Catalysis plays an important role in improving CO₂ desorption and thus reduces the energy consumption required for CO₂ separation technology.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is a schematic diagram of carbon dioxide separation setup (1: carbon dioxide cylinder; 2: nitrogen cylinder; 3: flow meter; 4: syringe pump; 5: heating tapes; 6: quartz tube reactor; 7: quartz wool; 8: sorbent; 9: quartz wool and notch block; 10: tube furnace; 11: water removal unit; 12: multi-gas analyzer; 13: data collection unit).

FIG. 2 is a graph of typical CO₂ sorption curves of blank tube and different solids (CO₂: 1 vol-%; H2O: 10 vol-%; gas flow rate: 0.3 L/min; sorption temperature: 60° C.; weight of pure K₂CO₃ or K—Fe sorbent: 1 g).

FIGS. 3A and 3B are SEM images of FeOOH (A) and the synthesized K—Fe sorbent (B) at a magnification of 6000.

FIG. 4 is a graph showing the effect of K₂CO₃ content in K—Fe sorbent on CO₂ sorption capability. Conditions (CO₂: 1 vol-%; H2O: 10 vol-%; gas flow rate: 0.3 L/min; sorption temperature: 60° C.; weight of K—Fe sorbent: 1 g).

FIG. 5 is a graph showing the change of CO₂ sorption capacities with H₂O concentration (CO₂: 1 vol-%; gas flow rate: 0.3 L/min; sorption temperature: 60° C.; weight of K—Fe sorbent: 1 g).

FIG. 6 is a graph showing the effect of temperature on CO₂ sorption capacity (A: sorption profiles; B: sorption capacities; CO₂: 1 vol-%; H2O: 10 vol-%; gas flow rate: 0.3 L/min; weight of K—Fe sorbent).

FIG. 7 is a graph of the calculated Gibbs free energy and enthalpy changes of CO₂ sorption reaction with temperature.

FIG. 8 is a graph of the calculated equilibrium constants of CO₂ sorption reaction at different temperatures.

FIG. 9 is a graph of the multicycle use of 1 g sorbent for CO₂ sorption-desorption at two different desorption temperatures (sorption condition—CO₂: 1 vol-%; gas flow rate: 0.3 L/min; sorption temperature: 60° C.; sorbent regeneration conditions—temperature: 125 or 150° C.; time: 2 hrs; N₂ flow rate: 0.5 L/min).

FIG. 10 is a graph of the relationship between K—Fe sorbent size and pressure drop predicted with Ergun's law.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS I. Materials and Methods A. Reagent and Materials

All the reagents used in these experiments were of analytical or higher grade without further purification. Potassium carbonate was purchased from VWR International, LLC. (West Chester, Pa.). 4-20 mesh calcium chloride pellets were obtained from Fisher Scientific Inc. (Fair Lawn, N.J.). Nanoporous FeOOH was provided by Kemira Water Solution, Inc. (Bartow, Fla.). Deionized (DI) water was used for preparation of all the sorbents tested in this research.

B. Sorbent preparation and Characterization

The first step of preparing the K—Fe sorbent was to add 10 g FeOOH to 50 mL potassium carbonate solution (10 wt-%), followed by stirring the mixture with a magnetic stirrer at room temperature for 24 hrs and drying it in a rotary vacuum evaporator at 70° C. The morphological characteristics of the supporting material (FeOOH) and the synthesized K—Fe sorbent were analyzed using a Hitachi TM-1000 tabletop scanning electron microscope (SEM). The powder X-ray diffractions (XRD) of the fresh and spent sorbent were evaluated by Philips X′Pert diffractometer using Cu-Kα as its radiation resource under the chosen operation conditions (voltage: 40 kV; current: 40 mA; start angle: 5; end angle, 95; step size: 0.02; time per step: 1.00; scan speed: 0.02).

C. Co₂ Sorption/Desorption Apparatus

The experimental set-up used for separation of carbon dioxide during the research is illustrated in FIG. 1. Quarter inch Teflon tubing was used as the connection material in the flow system. Ultra high purity nitrogen 1 and carbon dioxide gas 2 (US Welding Inc., Denver, Colo.) were mixed through two flow meters 3 (Matheson Tri-Gas Inc., Montgomeryville, Pa.) to make the simulated flue gas stream for sorption tests. Water moisture was introduced to the simulated flue gas stream and its concentration was controlled by a syringe pump 4. The tubing from syringe pump 4 to reactor was wrapped with heating tapes 5 (Cole-Parmer Co., Vernon Hills, Ill.) to avoid water vapor condensation. A three-eighth inch quartz tube 6 with a notch in it was used as the sorption-desorption reactor. Two pieces of quartz wool 7, 9 were placed at the two sides of the sorbent bed 8 to hold sorbent during sorption and sorbent regeneration. Sorption temperatures in the reactor were controlled by a F21135 tube furnace 10 (Barnstead International, Dubuque, Iowa). The water in the post-adsorption gas steam was eliminated by a water removal unit 11 prior to CO₂ analysis. The CO₂ concentration of the inlet/outlet gas stream was measured by a ZRE infrared gas analyzer 12 (Fuji Electric System Co. Ltd., Tokyo, Japan), and the sorption and desorption data were collected with a DataChart 3000 recorder 13 (Monarch Instrument Inc., Amherst, N.H.).

II. Results and Discussion A. Factors Affecting Co₂ Sorption 1. Dispersion of K₂CO₃ on Nanoporous FeOOH

Impregnating an active compound onto the surface of a porous matrix can improve the sorption capacity and selectivity of a sorbent for a targeted pollutant or contaminant. Hayashi et al. showed that the CO₂ sorption capacities of the supported K₂CO₃ sorbents are closely related to the characteristics of the support matrixes and the distributions of potassium carbonate on the surfaces of the porous matrixes. (Hayashi, H.; Taniuchi, J.; Furuyashiki, N.; Sugiyama, S.; Hirano, S.; Shigemoto, N.; Nonaka, T. Ind. Eng. Chem. Res. 1998, 37, (1), 185-191). Good supporting materials should not only possess large surface areas but also large pore volumes, both of which are prerequisites for preparation of high-capacity CO₂ sorbents. (Zhao, C.; Chen, X.; Zhao, C. Ind. Eng. Chem. Res. 2010, 49, (33)). The supporting material used for this research, FeOOH, is inexpensive, granular, highly porous, mechanically strong, and widely available. It has extremely large BET (Brunauer, Emmet, and Teller) surface area (˜200 m²/g) compared to other inorganic counterparts.

The sorption tests of blank reactor, pure FeOOH (supporting material), K₂CO₃ powder, and the K—Fe sorbent were run to check the degrees to which they adsorb CO₂. The test results are shown in FIG. 2. Obviously, the sorption capacities of blank reactor and pure FeOOH are negligible compared to that of K₂CO₃ powder, especially that of the K—Fe sorbent. The maximum CO₂ sorption efficiency of pure K₂CO₃ powder is only about 15% while K—Fe-sorbent can achieve as high as a 100% CO₂ sorption efficiency.

The total carbon dioxide sorption capacities of those four solids are calculated based on their sorption profiles, and listed in Table 1.

TABLE 1 Comparison of blank reactor, pure FeOOH and K₂CO, and synthesized K—Fe sorbent in CO₂ adsorption (CO₂: 1 vol-%; H₂O: 10 vol-%; gas flow rate: 0.3 L/min; sorption temperature: 60° C.; weight of pure K₂CO₃ or K—Fe sorbent: 1 g) CO₂ sorption capacity percentage of reacted Solids (mg CO₂/g-sorbent) K₂CO₃ (%) Tube reactor 0 — FeOOH* 0.16 ± 0.02 — K₂CO₃* 2.01 ± 0.42  0.57 ± 0.12 K—Fe sorbent** 49.20 ± 3.96  46.83 ± 3.77

The total CO₂ sorption capability is defined as the amount of CO₂ adsorbed per gram of K₂CO₃ powder or K—Fe sorbent from a gas stream until the carbon dioxide concentration in the outlet gas stream reaches 1 vol-% of the inlet or initial CO₂ concentration of the simulated flue gas stream. The supporting material, raw FeOOH, has almost no CO₂ adsorption even though it has a similar pore structure to that of the modified FeOOH or the FeOOH loaded with K₂CO₃ or the K—Fe sorbent as shown in FIGS. 3A and 3B. The sorption capability of K₂CO₃ powder is only 2.0 mg CO₂/g-K₂CO₃ under the given experimental conditions. However, the CO₂ sorption capacity of the K—Fe sorbent is 49 mg CO₂/g-sorbent, about seventy times higher than that of K₂CO₃ powder. Therefore, dispersing K₂CO₃ onto the surface of the porous supporting material FeOOH leads to dramatic improvement of CO₂ sorption due to the high accessibility of potassium carbonate on the surface of nanoporous FeOOH.

The effect of the loading amount of K₂CO₃ on the surface of FeOOH on total CO₂ sorption capacity of the finished K—Fe sorbent can be observed in FIG. 4. The capability of K—Fe sorbent reaches its peak when the loading amount of K₂CO₃ is 33.3 wt-% of the K—Fe sorbent under the given experimental conditions. Without being limited, one theory is that overdoing K₂CO₃ on FeOOH affects the pore structure of the finished K—Fe sorbent and consequently reduces the accessibility of K₂CO₃ and thus CO₂ sorption efficiency as well as total CO₂ sorption capacity.

2. H₂O Concentration

Moisture, usually present in the actual flue gases, can be as high as 8-17 vol-% varying from one power plant to another. It often has negative effects on the CO₂ sorption capacities of conventional sorbents such as zeolites, silica and molecular sieves.

However, unlike most of the conventional solid CO₂ sorbents the K—Fe sorbent needs an adequate amount of water for its efficient CO₂ adsorption as demonstrated in the following sorption reaction

$\begin{matrix} {{K_{2}{CO}_{3}} + {H_{2}O} + {{{CO}_{2}\overset{K}{}2}{KHCO}_{3}}} & ({R1}) \end{matrix}$

where K is the sorption equilibrium constant of R1 under certain conditions. According to stoichiometry, one mole of K₂CO₃ can react with one mole of CO₂ and one mole of H₂O to form two moles of KHCO₃. FIG. 5 shows that the total CO₂ sorption capability increases from 24 mg CO₂/g-sorbent to 49 mg CO₂/g-sorbent when water concentration increases from 1 to 10 vol-%, which means that water can enhance CO₂ sorption considerably. The fact can be explained by looking into the possible pathways of R1 as shown below

$\begin{matrix} {{CO}_{2} + {H_{2}{OH^{+}}} + {HCO}_{3}^{-}} & ({R2}) \\ {{K_{2}{{CO}_{3}\overset{H_{2}O}{}2}K^{+}} + {CO}_{3}^{2 -}} & \left( {R\; 3} \right) \\ {H^{+} + {{CO}_{3}^{2 -}{HCO}_{3}^{-}}} & ({R4}) \\ {{2K^{+}} + {2{{HCO}_{3}^{-}2}{{KHCO}_{3}.}}} & ({R5}) \end{matrix}$

R1 and R2 show that the presence of H₂O is necessary for the subsequent occurrences of R4 and R5. Considering the fact that H₂O has low CO₂ dissolving ability and K₂CO₃ is a strong-base but weak-acid salt, it is easy to imagine that H₂O plays a very important role in the overall CO₂ adsorption performance of the K—Fe sorbent. More water leads to more CO₂ to dissolve and thus generate more H⁺ and HCO₃ ⁻ which subsequently combines with K⁺ to form more adsorption product, KHCO₃. An adequate amount of water is also necessary for the disassociation of K₂CO₃ into CO₃ ² and K⁺, which are the reacting species of R4 and R5, respectively.

3. Sorption Temperature

CO₂ adsorption tests were conducted in the temperature range of 40-110° C. to assess the effect of temperature on the total CO₂ capture capability of the K—Fe sorbent. The sorption profiles and the corresponding CO₂ sorption capacities of the sorbent at different temperatures are presented in FIGS. 6A and 6B, respectively. CO₂ sorption capability decreases considerably with the increase of adsorption temperature. The total CO₂ capture capability drops from ˜88 mg CO₂/g-sorbent (very close to the theoretical CO₂ adsorption capacity in term of K₂CO₃ loaded per gram of sorbent) to 13 mg CO₂/g-sorbent when sorption temperature increases from 40° C. to 110° C. The change trend is consistent with what is predicted by thermodynamic theory. The Gibbs free energy and enthalpy changes of the sorption reaction R1 within the sorption temperature range are calculated and presented in FIG. 7. From FIG. 7 it is seen that the sorption reaction is exothermic and ΔH_(R1) becomes more negative with the increase of temperature while ΔG_(R1) considerably increases with the temperature even though its values are still negative within the sorption temperature range. Based on

ΔG=− RT LnK  (E1)

the Ln K and sorption temperature relationships are calculated and presented in FIG. 8. It is clear that K values decrease and the CO₂ partial pressures (p_(CO) ₂ ) at equilibrium increase dramatically with the elevation of sorption temperatures due to

K=p _(CO) ₂ ⁻¹  (E2)

as expected. Therefore, the sorbent experiences a large decrease in the CO₂ sorption capacity when sorption temperature increases from 40° C. to 110° C.

Catalytic CO₂ Desorption and Sorbent Regeneration

An ideal sorbent should not only have high mechanical strength, activity, selectivity and sorption capacity but also be regenerable for multicycle uses in a fixed-bed or fluidized bed reactor. The multicycle CO₂ capture capacities of the sorbents of the present invention at two different regeneration temperatures (125° C. and 150° C.) were evaluated and the results are shown in FIG. 9.

Three major facts are observed in FIG. 9. The first one is that the sorption capabilities of the sorbent decease gradually in the first few sorption-desorption cycles at both regeneration temperatures (125° C. and 150° C.) until they reach stable levels. XRD studies were conducted to understand the causes of the initial drops. The XRD images of both fresh and spent sorbents show similar structures, which are largely amorphous with small traces of crystalloids. In other words, no new species or structures are observed on the surface of the regenerated sorbent.

Another observed fact is that the sorbent is completely regenerable even at 125° C. and demonstrates the constant sorption capacity as shown in FIG. 9, which indicates that the nanoporous FeOOH may not only function as a good K₂CO₃ supporting material for synthesis of the K—Fe sorbent but also as a catalyst for CO₂ desorption during spent sorbent regeneration process since according to Lee the KHCO₃ decomposition reaction at 125° C. even at 150° C. should be very slow. (Lee, K. S.; Kim, I. W. J. Phys. Soc. Jpn. 2001, 70, (12), 3581-3584). The activation energy of KHCO₃ decomposition is as high as 92.5 kJ/mol. (Tanaka, H. Journal Therm. Anal 1987, 32, (2), 521-526). Therefore, catalysis must exist during the CO₂ desorption from the surface of the spent K—Fe sorbent. According to the Arrhenius equation

$\begin{matrix} {k_{{KHCO}_{3}\text{-}{decompoistion}} = {A*^{{- E}/{RT}}}} & ({E3}) \end{matrix}$

where k_(KHCO) ₃ _(-decomposition) is the apparent CO₂ the desorption rate constant, A represents the pre-exponential factor, R denotes 8.314 (J.K⁻¹.mol⁻¹), E is activation energy (J.mol⁻¹), and T is the reaction temperature (K), increasing A and decreasing E are the only two ways to increase k_(KHCO) ₃ _(-decomposition) or improve CO₂ desorption kinetics that can be realized by using nanoporous FeOOH in this research. Compared to conventional solid supporting materials, nanoporous FeOOH, on which nucleate KHCO₃ resulting from CO₂ adsorption disperses, could provide much more contact opportunities for KHCO₃ molecules on the surface of the spent sorbent, thus significantly increasing the pre-exponential factor (A) in E3. Furthermore, nanoporous FeOOH is well known for its abilities in reducing activation energy required for various reactions. It is reasonable to assume that nanoporous FeOOH could reduce the activation energy of KHCO₃ decomposition by 3-15%. Based on the reported E for KHCO₃ decomposition and the assumed activation energy reduction percentages of FeOOH, 3-15%, the potential increase ratios of the KHCO₃ decomposition rate constant (k_(KHCO) ₃ _(-decomposition)) in E3 at 398 K (125° C.) due to the use of the FeOOH and thus the reduction of E are estimated and shown in Table 2.

TABLE 2 Catalytic effect of FeOOH on KHCO₃ decomposition rate constants due to its potential in reducing the reaction's activation energy m (%) 3 6 9 12 15 $e{\frac{E_{{with} - {FeOOH}}}{{RT}_{{KHCO}_{3} - {decomposition}}}/e}\frac{E_{{without} - {FeOOH}}}{{RT}_{{KHCO}_{3} - {decomposition}}}$ 2.3 5.4 12.4 28.6 66.2 *Note: E_(with-FeOOH) = (100%-m) *E_(without-FeOOH); m is the assumed reduction percentage of the reported activation energy of CO₂ decomposition, 92.5 (kJ/mol) (Tanaka et al., 1987); T_(KHCO3-decomposition) = 398K.

It is clear that the importance of FeOOH as a catalyst in CO₂ desorption could not be neglected since it could significantly accelerate the decomposition of KHCO₃ even when it only reduces the activation energy of CO₂ desorption reaction by 5%.

FeOOH is well known for its strong abilities in physicochemical complexion within aqueous environment with anions such as H₂AsO₄ ⁻, which is the basis for its wide application in water and wastewater treatment. The reverse reaction of R4 or the disassociation of HCO₃ ⁻ within an alkaline environment is not an easy one but, without the help of catalysts, it is one of the necessary steps in overall CO₂ desorption process. The use of FeOOH with huge Lewis acid sites could lead to a different HCO₃ ⁻ disassociation or CO₂ desorption pathway since FeOOH can complex with HCO₃ ⁻ (a Lewis base) and then dissociate it into CO₂ and OH⁻. The resultant OH⁻ can then easily combine with the H⁻ on the left side of R4 to accelerate the shift of R4 towards its left side according to Le Châtelier's principle, and thus accelerate overall CO₂ desorption process.

The last phenomenon demonstrated in FIG. 9 is that the sorbent has better multicycle performance at 125° C. than at 150° C. since the stable CO₂ sorption capacity at 125° C. is ˜30 mg/g-sorbent, about a 50% increase compared to that at 150° C. The rate law needs to be resorted to explain the phenomenon. Assuming that the decomposition rate (r_(KHCO) ₃ _(-decomposition)) of KHCO₃ can be expressed as

r _(KHCO) ₃ _(-decomposition) =k _(KHCO) ₃ _(-decomposition) C _(KHCO) ₃ ^(n) ^(KHCO) ³   (E4)

where C_(KHCO) ₃ is the mole concentration of KHCO₃ on FeOOH (mol-KHCO₃/m²-FeOOH), n_(KHCO) ₃ is the apparent CO₂ desorption reaction order with respect to KHCO₃. The difference can be attributed to the variations of between r_(KHCO) ₃ _(-decomposition,125° C.) and r_(KHCO) ₃ _(decomposition,150° C.) can be attributed to the variations of k_(KHCO) ₃ _(-decomposition) and n_(KHCO) ₃ _(-decomposition) with temperature. KHCO₃ decomposition is a multistep heterogeneous reaction process and k_(KHCO) ₃ _(-decomposition) is mainly determined by the rate controlling step. The adsorption of HCO₃ ⁻ on FeOOH surface should be the slowest step and is weaker at 150° C. than at 125° C., possibly leading to k_(KHCO) ₃ _(-decomposition,125° C.)>k_(KHCO) ₃ _(-decomposition,150° C.), which partially contributes to the fact that the KHCO₃ decomposition rate or the quantity of the desorbed CO₂ or the multicycle CO₂ sorption capacity at the regeneration temperature of 125° C. is higher than that at 150° C. as shown in FIG. 9. The value of n_(KHCO) ₃ may also change with temperature since the formation and growth of nuclei of K₂CO₃ during KHCO₃ decomposition or CO₂ desorption process are, according to Lee, et al. (2001) and Tanaka, et al, (1987), very complicated and due to the fact that part of KHCO₃ exists in its dimeric form. Phase change within the dimer occurs along with the thermal decomposition of KHCO₃. The migration of the protons within the dimer in forms of intrabond and interbond jumps can be significantly affected by temperature and the structure of the surface on which the dimer stays. The undersaturation of the coordination environment of oxygen, hydroxyl bonds and hydrogen bonds in the FeOOH structure make it highly affinitive to protons in the dimer. With these factors considered, n_(KHCO) ₃ _(,125° C.)might be larger than n_(KHCO) ₃ _(,150° C.), which can also partially explain why the KHCO₃ decomposition rate or the quantity of the desorbed CO₂ or the multicycle CO₂ sorption capacity at the regeneration temperature of 125° C. is higher than that at 150° C. as shown in FIG. 9.

Solid sorbents containing alkali or alkali earth metals for CO₂ adsorption have been frequently reported and recommended to be used for CO₂ separation due to their low prices and wide availabilities, and among them is CaO. However, the reaction between CaO and CO₂ is a very slow one at low temperature and usually needs to be operated at 500-600° C. and regenerated at temperatures higher than 850° C. (Abu-Zahra, M. R. M.; Schneiders, L. H. J.; Niederer, J. P. M.; Feron, P. H. M.; Versteeg, G. F. Int. J. Greenhouse Gas Control 2007, 1, (1), 37-46). The robust K—Fe sorbent synthesized in this research can effectively adsorb CO₂ at temperatures in the range of 50-70° C. in the presence of moisture, which matches the conditions of flue gases in power plants, and can be generated at 125° C., which is achievable with the heat of waste gases in power plants. Therefore, the K—Fe sorbent is superior to Ca and Mg based solid sorbents from the viewpoints of CO₂ sorption-desorption operation optimization and waste heat recovery viewpoints.

Compared to most of the recently reported solid CO₂ sorbents based on organic compounds, the unit CO₂ sorption capacity of the K—Fe sorbent is lower. However, the preparation process of the K—Fe sorbent is simple and only needs two stable and inexpensive inorganic compounds, K₂CO₃ and FeOOH, while organic sorbents are synthesized with much more expensive materials and require the use of a lot of solvents during their preparation processes.

Sorbent Size and Pressure Drop

In addition to CO₂ desorption or spent sorbent regeneration, another major factor affecting solid sorbent based CO₂ separation energy consumption is pressure drop in the sorbent bed. Pressure drops are considerably affected by the size of K—Fe sorbent and can be estimated using the below Ergun's equation

$\begin{matrix} {{150 \times \frac{\left( {1 - ɛ} \right)^{2}}{ɛ^{3}}\frac{\mu}{d_{p}^{2}}u} + {1.75\; \frac{1 - ɛ}{ɛ^{3}}\frac{\rho}{d_{p}}{u^{2}.}}} & {E5} \end{matrix}$

The characteristics of the K—Fe sorbent, the properties of flue gas and the desired configuration of the CO₂ adsorber allow us to assume that the interparticle porosity (ε) of the CO₂ sorption bed (fixed bed) is 0.6, flue gas viscosity (μ) is 5.4×10⁻⁴ kg/ms, interstitial velocity (u) is 0.75 m/s, and density of flue gas (ρ) is 0.85 kg/m³. Based on Ergun's law and the chosen parameters, the variations of pressure drop of flue gas stream in the fixed K—Fe sorbent bed with the diameters of the sorbent when the K—Fe sorbent is applied in power plants are predicated and presented in FIG. 10. FIG. 10 indicates that when a 10 m long, fixed-bed adsorber loaded with 5 mm K—Fe sorbents is constructed under the given conditions for CO₂ separation the total pressure drop of the flue gas during its passing the sorbent bed is only about 0.21 atm. Therefore, there is no need for a powerful blower to overcome the pressure drop of flue gas when the size of K—Fe sorbent is reasonably large. Finally, it should be mentioned that the K—Fe sorbent can not only be used in conventional fixed bed and radial flow fixed bed adsorbers but also in fluidized bed adsorbers due to its good mechanical properties.

III. Conclusions

The K—Fe-based sorbent synthesized with two widely available and low-priced materials can achieve high CO₂ sorption efficiency, is regenerable, and has good CO₂ sorption capacity. The catalytic function of the supporting material, FeOOH, could help reduce the energy consumption needed for CO₂ sorption. The inherent characteristics of the inorganic sorbent leads to low energy demand for overcoming the pressure drop of flue gas passing through the sorbent bed. Therefore, the K—Fe sorbent is promising since it can be potentially used for cost-effective CO₂ separation.

The foregoing description and drawings comprise illustrative embodiments of the present inventions. The foregoing embodiments and the methods described herein may vary based on the ability, experience, and preference of those skilled in the art. Merely listing the steps of the method in a certain order does not constitute any limitation on the order of the steps of the method. The foregoing description and drawings merely explain and illustrate the invention, and the invention is not limited thereto, except insofar as the claims are so limited. Those skilled in the art that have the disclosure before them will be able to make modifications and variations therein without departing from the scope of the invention. 

We claim:
 1. A sorbent for CO₂, comprising K₂CO₃ supported on FeOOH.
 2. A method of forming a sorbent for CO₂, comprising the steps of combining FeOOH with a solution of K₂CO₃, stirring to coat the FeOOH with the K₂CO₃ and drying.
 3. A method of removing CO₂ from a gas stream, comprising the step of passing the gas stream over a sorbent comprising K₂CO₃ supported on FeOOH. 